US3480417A - Hydrogen generator including a desulfurizer employing a feed-back ejector - Google Patents

Hydrogen generator including a desulfurizer employing a feed-back ejector Download PDF

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US3480417A
US3480417A US670640A US3480417DA US3480417A US 3480417 A US3480417 A US 3480417A US 670640 A US670640 A US 670640A US 3480417D A US3480417D A US 3480417DA US 3480417 A US3480417 A US 3480417A
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hydrogen
desulfurizer
steam
ejector
feedstock
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Herbert J Setzer
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Raytheon Technologies Corp
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United Aircraft Corp
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/007—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 in the presence of hydrogen from a special source or of a special composition or having been purified by a special treatment
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0405—Purification by membrane separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • C01B2203/1264—Catalytic pre-treatment of the feed
    • C01B2203/127—Catalytic desulfurisation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • a hydrogen generator including a desulfurization device upstream of a steam-reforming reactor. Recycle hydrogen is fed to an ejection device which is utilized as the means to feed at least the steam feedstream to the desulfurization device.
  • This invention relates to the removal of sulfur from hydrocarbon fuels in a hydrogen generation process, and more particularly to apparatus for utilizing feedback hydrogen for hydrodesulfurization.
  • Fuel cell powerplants are known to include two separate main sections.
  • the fuel cell proper reacts oxygen (or air) with hydrogen so as to form electricity together with waste hydrogen and air byproducts as well as heat and watery'.
  • the other portion of the fuel cell powerplant system is the hydrogen generator, which is sometimes referred to as a reformer.
  • the hydrogen generator portion of a 'fuel cell powerplant reacts a combination of hydrocarbon fuel and water to generate hydrogen gas for use in a fuel cell.
  • such systems utilize sulfur-free hydrocarbon fuels.
  • the usefulness of fuel cells is mitigated due to the need for special- Vrefining of the hydrocarbon fuel so as to achieve a lovvsulfur content prior to use in a fuel cell powerplant system.
  • the hydrogen generation process may include desulfurization.
  • An object of the present invention is the provision of nji'm'pr'oved desulfurizing. apparatus for use in a hydrogen generator capable of. operating with a feedstock having a ⁇ significant sulfur content.
  • the hydrogen content of hydrocarbon fuel being fed to a desulfurizer is increased by feeding hydrogen into the feedstock from a point downstreamof a reforming reactor (which generates hydrogen from the feedstock), the feedstock 'and hydrogen being mixed in an ejector.
  • the hydrogen may i be taken directly from the output of the steam reforming reactor or may be'taken from either a shift converter or a hydrogen utilization device which 'are downstream of BRIEF DESCRIPTION OF THE DRAWING FIG.
  • FIG. 2 is a schematic block diagram of an alternative embodiment of the present invention in which hydrogen fed back to the ejector is taken from the output of the shift converter;
  • FIG. 3 is a schematic block diagram of a hydrogen .generator system illustrating a modification of the ernbodiment of FIG. 1 in which no separator s utilized;
  • FIG. 4 is a schematic block diagram of a hydrogen generator system in accordance with the present invention illustrating a modification of the embodiment of FIG. 2 in which no separator is utilized; and s
  • FIG. 5 is a schematic block diagram of a hydrogen ygenerator system illustrating an embodiment in which anode effluent is ⁇ returned to the feedstock.
  • hydrogen is generated to be fed to the anode 10 of a fuel cell 12.
  • Hydrocarbon fuel is fe'd to a pump 14 where fuel at substantially atrnospheric pressure may be pumped up to anywhere from to 300 pounds per square inch absolute (p.s.i.a.), the particular pressure being dependent upon details of the system not involved herewith.
  • Another pump 16 is utilized to similarly pressurize water forl adrnixture with the hydrocarbon fuel at the input to a boiler 18.
  • the output of the lboiler is a superheated vapor which comprises a homogeneous mixture of steam and vapors of the hydrocarbons in the fuel.
  • This homogeneous mixture islfed to an ejector 20, the output of which is passed through a desulfurizer 22.
  • the desulfurizer may comprise a lcombination'catalyst and absorbant of any suitable type, but most preferably would be of the type described in a copending ⁇ application of the same assignee entitledxSulfur Removal From Hydrocarbons filed on even date herewith by H. J. Setzer and R. W. Whiting, Ser. No. 670,636.
  • the stock is fed to a steamreforming reactor 24, which is sometimes referred to as a dehydrogenation reactor.
  • the output of the steam reforming reactor 24 is fed to a shift converter 26 which in turn feeds a selective hydrogen diffusion membrane, such as a palladium-silver separator 28.
  • the palladiumsilver separator 28 provides nearly pure hydrogen to the anode 10 of the fuel cell 12, and also provides a bleed gas (comprising a mixture of hydrogen, carbon monoxide, carbon dioxide, methane and water) to a burner 30 which combines the bleed gas with air so as to generate heat, the heat being applied to operate the steam reforming reactor 24 and the boiler 18.
  • the process in the steam-reforming reactor 24 involves converting any of a number of different types of hydrocarbons which are in the feedstock by combining with steam so as to form hydrogen, carbon dioxide, carbon monoxide, and methane, along with some uncombned steam and traces of unconverted hydrocarbons of various types. Then the shift converter 26 in turn combines a high percentage of the carbon monoxide in the output of the steam-reforming reactor 24 with unreacted steam so as to form further hydrogen and carbon dioxide. Thus, the output of this shift converter includes a mixture of nearly all of the hydrogen which was available in the feedstock, some steam, together with carbon monoxide, carbon dioxide and methane.
  • a feedback line 32 may include a valve 34 for adjusting llow rates, and permits feeding generated hydrogen to the ejector 20 so that hydrogen will be inserted into the feedstock.
  • the valve 34 is connected to the output of the steam reforming reactor 24, so as topprovide molecular hydrogen (H2) into the feedstock at the input to the desulfurizer 22.
  • H2 molecular hydrogen
  • other components such as steam, carbon monoxide, carbon dioxide, and methane are also fed into the ejector 20, and thus through the desulfurizer 22. This results in various side reactions, but these are not important to the overall process involved and of no real consequence to the practice of the present invention.
  • a second embodiment of the invention utilizes the output of the shift converter 26 rather than the output of the steam reform reactor 24 for supplying hydrogen through the ejector 20 to the desulfurizer 22.
  • a greater hydrogen content is available so that a lesser amount of product need be diverted through the feedback line 32.
  • the choice of which embodiment (that of FIG. 1 or FIG. 2) is to be utilized depends upon the particular overall hydrogen generization system beingl designed, and may be determined to suit the operating parameters of any such a system.
  • FIG. 3 illustrates that the shift converter 26 and palladium-sliver separator 28 of FIGS. 1 and 2 may be eliminated if desired, without altering the present invention.
  • the invention relates to desulfurization in a hydrogen generator; the enhanced hydrogen generation which is achieved with a shift converter 26, as well as separation of the majority of the hydrogen from the remaining products with the palladiprn-silverseparator 28, need not be utilized if not desired.
  • FIG. 4 illustrates the fact that the silver-palladium separator 28 (FIGS. 1 and 2) may be eliminated without altering the present invention in either of its embodiments, the hydrogen output of the shift converter 26 being available for feedback through the ejector 20 into the feedstock at the input of the desulfurizer 22 whether or not the seperator 28 is used.
  • the pumps 14, 16 may be run .at a lQWr pressure or eliminated altogether. How- 4 ever, desulfurization in a catalyst absorber works better at pressures up to 300 p.s.i.a., so the pumps may be used if desired. In any event, this is a matter of detail design of a particular system, and not significant with respect to the present invention.
  • FIG. 5 is illustrated another'aspect of the present invention. That is, the effluent from the anode 10 of the fuel cell 12 may be fed back through the line 32 and valve 34 to the ejector 20 so as to supply hydrogen to assist in hydrodesulfurization.
  • This is most readily achieved as illustrated in FIG. 5 by eliminating the use of the palladium-silver separator 28 (see FIGS. l and 2) so that there is a low pressure drop through the system.
  • the pressure at the outlet of the anode 10 will not be too low with respect to the pressure at the output of fthe boiler 18 so that the ejector 20 will properly function to draw hydrogen into the feedstock at the input to the desulfurizer 22.
  • FIG. 5 is illustrated another'aspect of the present invention. That is, the effluent from the anode 10 of the fuel cell 12 may be fed back through the line 32 and valve 34 to the ejector 20 so as to supply hydrogen to assist in hydrodesulfurization.
  • This is most readily achieved as illustrated in
  • the portion of the effluent of the anode 10 which is not fed back to the ejector may be burned in the burner 30 so as to supply heat for the steam reforming reactor 24 and the boiler 18.
  • the providing of fuel to the burner 30 is not germano to the present invention, and other arrangements may be selected from among those known to the art for disposing of anode effluent and for providing fuel to the burner 30.
  • the basic premise of one aspect of the present invention is to utilize an ejector to return hydrogen generated in a hydrogen generator to enrich the feedstock which is fed through the hydrogen generator, the hydrogen being taken from a point in the system at essentially the same pressure as the input to the desulfurizer, thereby to avoid compression of gaseous hydrogen.
  • liquid fuel is considered herein, gaseous fuel could also be used.
  • the hydrogen would then most advantageously be mixed with steam prior to the admixing of steam and gaseous fuel to form the feedstock.
  • a hydrogen generator of the type which ygenerates hydrogen through the reaction of steam and hydrocarbon fuels comprising:
  • an ejector for receiving at least the steam portion of the feedstock, the output of said ejector being fed to said desulfurizer, said desulfurizer receiving hydrocarbon fuel in gaseous form as well as steam;
  • the hydrogen generator accordinging to claim 1 in- 3,350,176 10/ 1967 Green et al 48-214 XR cluding a shift converter, the input of which is connected to the output of said steam reforming reactor, and where- 5 FOREIGN PATENTS in said feedback line is connected to the output of said 992,161 5/1965 Great Britain,v shift converter.

Description

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CROSS-REFERENCE TO RELATED APPLICATIONS BACKGROUND 0F THE INVENTION Field of invention This invention relates to the removal of sulfur from hydrocarbon fuels in a hydrogen generation process, and more particularly to apparatus for utilizing feedback hydrogen for hydrodesulfurization.
Description of the prior art Fuel cell powerplants are known to include two separate main sections. The fuel cell proper reacts oxygen (or air) with hydrogen so as to form electricity together with waste hydrogen and air byproducts as well as heat and watery'. The other portion of the fuel cell powerplant system is the hydrogen generator, which is sometimes referred to as a reformer. The hydrogen generator portion of a 'fuel cell powerplant reacts a combination of hydrocarbon fuel and water to generate hydrogen gas for use in a fuel cell. Inv the prior art, such systems utilize sulfur-free hydrocarbon fuels. However, the usefulness of fuel cells is mitigated due to the need for special- Vrefining of the hydrocarbon fuel so as to achieve a lovvsulfur content prior to use in a fuel cell powerplant system. In order for the efficiencies of a fuel cell to reach maximum value, many applications of fuel cells would be enhanced by the ability of the fuel cell to use commercially available hydrocarbon fuels such as jet engine fuel, unleaded gasolines, natural gas, etc., as the source of hydrocarbons for hydrogen generation. In order to permit the use of hydrocarbon fuels which have not been specially refined or processed so as to remove the sulfur, the hydrogen generation process may include desulfurization.
SUMMARY OF THE INVENTION An object of the present invention is the provision of nji'm'pr'oved desulfurizing. apparatus for use in a hydrogen generator capable of. operating with a feedstock having a` significant sulfur content.
3,480,417y Patented Nov. 25, 1969 ice"` According to the present invention, the hydrogen content of hydrocarbon fuel being fed to a desulfurizer is increased by feeding hydrogen into the feedstock from a point downstreamof a reforming reactor (which generates hydrogen from the feedstock), the feedstock 'and hydrogen being mixed in an ejector. The hydrogenmay i be taken directly from the output of the steam reforming reactor or may be'taken from either a shift converter or a hydrogen utilization device which 'are downstream of BRIEF DESCRIPTION OF THE DRAWING FIG. l is a schematic block diagram of a hydrogen generator system in accordance with the present invention illustrating a first embodiment in which hydrogen is fed to the ejector from a point between the reform reactor and the shift converter; FIG. 2 is a schematic block diagram of an alternative embodiment of the present invention in which hydrogen fed back to the ejector is taken from the output of the shift converter;
FIG. 3 is a schematic block diagram of a hydrogen .generator system illustrating a modification of the ernbodiment of FIG. 1 in which no separator s utilized;
FIG. 4 is a schematic block diagram of a hydrogen generator system in accordance with the present invention illustrating a modification of the embodiment of FIG. 2 in which no separator is utilized; and s FIG. 5 is a schematic block diagram of a hydrogen ygenerator system illustrating an embodiment in which anode effluent is `returned to the feedstock.
DESCRIPTION OF THE PREFERRED EMBODIMENT Referring now to FIG. 1, hydrogen is generated to be fed to the anode 10 of a fuel cell 12. Hydrocarbon fuel is fe'd to a pump 14 where fuel at substantially atrnospheric pressure may be pumped up to anywhere from to 300 pounds per square inch absolute (p.s.i.a.), the particular pressure being dependent upon details of the system not involved herewith. Another pump 16 is utilized to similarly pressurize water forl adrnixture with the hydrocarbon fuel at the input to a boiler 18. The output of the lboiler is a superheated vapor which comprises a homogeneous mixture of steam and vapors of the hydrocarbons in the fuel. This homogeneous mixture islfed to an ejector 20, the output of which is passed through a desulfurizer 22. The desulfurizer may comprise a lcombination'catalyst and absorbant of any suitable type, but most preferably would be of the type described in a copending` application of the same assignee entitledxSulfur Removal From Hydrocarbons filed on even date herewith by H. J. Setzer and R. W. Whiting, Ser. No. 670,636. From the desulfurizer 22, the stock is fed to a steamreforming reactor 24, which is sometimes referred to as a dehydrogenation reactor. The output of the steam reforming reactor 24 is fed to a shift converter 26 which in turn feeds a selective hydrogen diffusion membrane, such as a palladium-silver separator 28. The palladiumsilver separator 28 provides nearly pure hydrogen to the anode 10 of the fuel cell 12, and also provides a bleed gas (comprising a mixture of hydrogen, carbon monoxide, carbon dioxide, methane and water) to a burner 30 which combines the bleed gas with air so as to generate heat, the heat being applied to operate the steam reforming reactor 24 and the boiler 18. The boiler 18,y the steam assignee entitled Method and Apparatus for Generating Hydrogen From Liquid Hydrogen Containing Feedstocks, led on Aug. 3, 1965 by Richard F. Buswell et al., Ser. No. 476,906. Briefly described, the process in the steam-reforming reactor 24 involves converting any of a number of different types of hydrocarbons which are in the feedstock by combining with steam so as to form hydrogen, carbon dioxide, carbon monoxide, and methane, along with some uncombned steam and traces of unconverted hydrocarbons of various types. Then the shift converter 26 in turn combines a high percentage of the carbon monoxide in the output of the steam-reforming reactor 24 with unreacted steam so as to form further hydrogen and carbon dioxide. Thus, the output of this shift converter includes a mixture of nearly all of the hydrogen which was available in the feedstock, some steam, together with carbon monoxide, carbon dioxide and methane. There are also traces of various hydrocarbons which have not been recombined. Thus, hydrogen is converted'not only from the hydrocarbon fuel, but also from the water which is combined therewith to form the feedstock. This is described in great detail in the aforementioned copending Buswell et al. application.
As is well known, the presence of hydrogen in a hydrocarbon feedstock has a beneficial effect on the desulfurization reaction.
According to the present invention, a feedback line 32 may include a valve 34 for adjusting llow rates, and permits feeding generated hydrogen to the ejector 20 so that hydrogen will be inserted into the feedstock. In accordance with the embodiment of the invention shown in FIG. 1, the valve 34 is connected to the output of the steam reforming reactor 24, so as topprovide molecular hydrogen (H2) into the feedstock at the input to the desulfurizer 22. Of course, other components such as steam, carbon monoxide, carbon dioxide, and methane are also fed into the ejector 20, and thus through the desulfurizer 22. This results in various side reactions, but these are not important to the overall process involved and of no real consequence to the practice of the present invention.
Referring now to FIG. 2, a second embodiment of the invention utilizes the output of the shift converter 26 rather than the output of the steam reform reactor 24 for supplying hydrogen through the ejector 20 to the desulfurizer 22. In this case, a greater hydrogen content is available so that a lesser amount of product need be diverted through the feedback line 32. The choice of which embodiment (that of FIG. 1 or FIG. 2) is to be utilized depends upon the particular overall hydrogen generization system beingl designed, and may be determined to suit the operating parameters of any such a system.
The embodiment disclosed in FIG. 3 illustrates that the shift converter 26 and palladium-sliver separator 28 of FIGS. 1 and 2 may be eliminated if desired, without altering the present invention. In other words, the invention relates to desulfurization in a hydrogen generator; the enhanced hydrogen generation which is achieved with a shift converter 26, as well as separation of the majority of the hydrogen from the remaining products with the palladiprn-silverseparator 28, need not be utilized if not desired.
The embodiment shown in FIG. 4 illustrates the fact that the silver-palladium separator 28 (FIGS. 1 and 2) may be eliminated without altering the present invention in either of its embodiments, the hydrogen output of the shift converter 26 being available for feedback through the ejector 20 into the feedstock at the input of the desulfurizer 22 whether or not the seperator 28 is used.
In the embodiments of FIGS. 3 and 4, since no palladium-silver separator is used, the pumps 14, 16 may be run .at a lQWr pressure or eliminated altogether. How- 4 ever, desulfurization in a catalyst absorber works better at pressures up to 300 p.s.i.a., so the pumps may be used if desired. In any event, this is a matter of detail design of a particular system, and not significant with respect to the present invention.
In FIG. 5 is illustrated another'aspect of the present invention. That is, the effluent from the anode 10 of the fuel cell 12 may be fed back through the line 32 and valve 34 to the ejector 20 so as to supply hydrogen to assist in hydrodesulfurization. This is most readily achieved as illustrated in FIG. 5 by eliminating the use of the palladium-silver separator 28 (see FIGS. l and 2) so that there is a low pressure drop through the system. Thus, the pressure at the outlet of the anode 10 will not be too low with respect to the pressure at the output of fthe boiler 18 so that the ejector 20 will properly function to draw hydrogen into the feedstock at the input to the desulfurizer 22. As illustrated in FIG. 5, the portion of the effluent of the anode 10 which is not fed back to the ejector may be burned in the burner 30 so as to supply heat for the steam reforming reactor 24 and the boiler 18. However, the providing of fuel to the burner 30 is not germano to the present invention, and other arrangements may be selected from among those known to the art for disposing of anode effluent and for providing fuel to the burner 30.
It should be understood that the basic premise of one aspect of the present invention is to utilize an ejector to return hydrogen generated in a hydrogen generator to enrich the feedstock which is fed through the hydrogen generator, the hydrogen being taken from a point in the system at essentially the same pressure as the input to the desulfurizer, thereby to avoid compression of gaseous hydrogen.
Although liquid fuel is considered herein, gaseous fuel could also be used. The hydrogen would then most advantageously be mixed with steam prior to the admixing of steam and gaseous fuel to form the feedstock.
Although the embodiments herein illustrate use of hydrogen in the anode of a fuel cell, it should be understood by those skilled in the art that the principle of the present invention, which relates to diffusion of feedback hydrogen for desulfurization of hydrocarbon feedstock is equally valuable without regard to the use to which the generated hydrogen is to be put.
Although the invention has been shown and described with respect to preferred embodiments thereof, it should be understood by those skilled in the art that the foregoing and other changes and omissions in the form and detail thereof may be made therein without departing from the spirit and scope of the invention, which is to be limited and defined only as set forth in the following claims.
Having thus described typical embodiments of the invention, that which I claim as new and desire to secure by Letters Patent of the United States is:
1. A hydrogen generator of the type which ygenerates hydrogen through the reaction of steam and hydrocarbon fuels, comprising:
a steam reforming reactor; desulfurizing means connected with said steam reforming reactor so that the output of said desulfurizing means is applied as the input to said steam reforming reactor; l
an ejector for receiving at least the steam portion of the feedstock, the output of said ejector being fed to said desulfurizer, said desulfurizer receiving hydrocarbon fuel in gaseous form as well as steam; and
a feedback line connected at a point in said system downstream Vof said steam reforming reactor for passing products including molecular hydrogen to a second input of said ejector, whereby at least molecular hydrogen is intermixed with at least the stream portion of the feedstock of said hydrogen generator. 2. The hydrogen generator according to claim 1 where- 5 6 in said -feedback line is connected at the output of said 3,178,272 4/ 1965 Dent et al. 48-2l3 stream reforming reactor. 3,278,268 10/ 1966 Pfeifer-le 23--212 3. The hydrogen generator.according to claim 1 in- 3,350,176 10/ 1967 Green et al 48-214 XR cluding a shift converter, the input of which is connected to the output of said steam reforming reactor, and where- 5 FOREIGN PATENTS in said feedback line is connected to the output of said 992,161 5/1965 Great Britain,v shift converter.
References Cited MORRIS 0. WOLK, Primary Examiner UNITED STATES PATENTS BARRY S. RICHMAN, Assistant Examiner y 2,773,561 12/1956 Hunter 23--210 XR m 2,902,440 9/1959 Beumer e: al.- U-S- Cl- ,X-R- 3,019,096 l/ 1962 Milbome 48-213 232l0, 212; 48-2l4; 208-209
US670640A 1967-09-26 1967-09-26 Hydrogen generator including a desulfurizer employing a feed-back ejector Expired - Lifetime US3480417A (en)

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3725252A (en) * 1970-07-27 1973-04-03 Universal Oil Prod Co Desulfurization with subsequent h{11 s absorption
US3961986A (en) * 1975-11-20 1976-06-08 United Technologies Corporation Method and apparatus for controlling the fuel flow to a steam reformer in a fuel cell system
US4181503A (en) * 1978-10-30 1980-01-01 United Technologies Corporation Process for alternately steam reforming sulfur containing hydrocarbons that vary in oxygen content
US4309359A (en) * 1976-12-15 1982-01-05 Imperial Chemical Industries Limited Energy process in methanol synthesis
US20090035622A1 (en) * 2007-07-31 2009-02-05 Battelle Memorial Institute Systems and methods for reducing organic sulfur components in hydrocarbon fuels
US20120040256A1 (en) * 2009-12-25 2012-02-16 Yukimune Kani Hydrogen generator and fuel cell system
US9583776B2 (en) 2011-09-02 2017-02-28 Battelle Memorial Institute Sweep membrane separator and fuel processing systems

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2154600A (en) * 1984-02-23 1985-09-11 British Gas Corp Producing and purifying methane
DK201500463A1 (en) * 2015-08-12 2016-08-29 Haldor Topsoe As Chemical recuperation of hydrocarbonic fuel using concentrated solar power

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2773561A (en) * 1955-05-02 1956-12-11 Atlantic Refining Co Silver-palladium film for separation and purification of hydrogen
US2902440A (en) * 1957-07-12 1959-09-01 Gulf Research Development Co Process for utilizing impure hydrogen stream in hydrogenation reactions
US3019096A (en) * 1959-05-13 1962-01-30 United Eng & Constructors Inc Process for fluid catalytic reforming of hydrocarbons to gas
US3148031A (en) * 1961-02-08 1964-09-08 Union Carbide Corp Method for separating and purifying hydrogen by permeation
US3178272A (en) * 1954-12-07 1965-04-13 Gas Council Gasification of hydrocarboncontaining oils
GB992161A (en) * 1963-04-05 1965-05-19 Exxon Research Engineering Co Improvements in hydrocarbon gasification processes
US3278268A (en) * 1962-08-15 1966-10-11 Engelhard Ind Inc Method for hydrogen production
US3350176A (en) * 1964-03-24 1967-10-31 Engelhard Ind Inc Hydrogen generator

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3178272A (en) * 1954-12-07 1965-04-13 Gas Council Gasification of hydrocarboncontaining oils
US2773561A (en) * 1955-05-02 1956-12-11 Atlantic Refining Co Silver-palladium film for separation and purification of hydrogen
US2902440A (en) * 1957-07-12 1959-09-01 Gulf Research Development Co Process for utilizing impure hydrogen stream in hydrogenation reactions
US3019096A (en) * 1959-05-13 1962-01-30 United Eng & Constructors Inc Process for fluid catalytic reforming of hydrocarbons to gas
US3148031A (en) * 1961-02-08 1964-09-08 Union Carbide Corp Method for separating and purifying hydrogen by permeation
US3278268A (en) * 1962-08-15 1966-10-11 Engelhard Ind Inc Method for hydrogen production
GB992161A (en) * 1963-04-05 1965-05-19 Exxon Research Engineering Co Improvements in hydrocarbon gasification processes
US3350176A (en) * 1964-03-24 1967-10-31 Engelhard Ind Inc Hydrogen generator

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3725252A (en) * 1970-07-27 1973-04-03 Universal Oil Prod Co Desulfurization with subsequent h{11 s absorption
US3961986A (en) * 1975-11-20 1976-06-08 United Technologies Corporation Method and apparatus for controlling the fuel flow to a steam reformer in a fuel cell system
US4309359A (en) * 1976-12-15 1982-01-05 Imperial Chemical Industries Limited Energy process in methanol synthesis
US4181503A (en) * 1978-10-30 1980-01-01 United Technologies Corporation Process for alternately steam reforming sulfur containing hydrocarbons that vary in oxygen content
US20090035622A1 (en) * 2007-07-31 2009-02-05 Battelle Memorial Institute Systems and methods for reducing organic sulfur components in hydrocarbon fuels
US20120040256A1 (en) * 2009-12-25 2012-02-16 Yukimune Kani Hydrogen generator and fuel cell system
US9334164B2 (en) * 2009-12-25 2016-05-10 Panasonic Intellectual Property Management Co., Ltd. Hydrogen generator and fuel cell system
US9583776B2 (en) 2011-09-02 2017-02-28 Battelle Memorial Institute Sweep membrane separator and fuel processing systems

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